Oil-converting process for the conversion and transformation of oils



THE CONVERSION'AND TRANSFORMATION OF OILS July 24, 1923.

5 Sheets-Sheet 1 J. H. ADAMS OIL CONVERTING PROCESS FOR Filed June 15 1916 kotukkv llVl/ENTOR July 24; 1923.

J. H. ADAMS OIL CONVERTING PROCESS FOR THE CONVERSION AND TRANSFORMATION OF OILS 5 Shgets-Sheet 2 Filed June 15 July 24, 1923. 1,462,677

J.HNADAMS OTlJ CONVERTING PROCESS FOR THE CONVERSION AND TRANSFORMATION OF OILS Filed Ju ne 15 1916 5 Sheets-Sheet 4 I VENTOR.

o 0 0 o 0 o o o o 0 0 O O O July 24, 1923.

J. H. ADAMS OIL CONVERTING PROCESS FOR THE CONVERSION AND TRANSFORMATION OF OILS 1916 I 5 Sheets-Sheet 5 Filed June 15 Patented July 24, 1923. i

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JOSEPH H. ADAMS, F FLATBUSH, NEW YORK, ASSIGNOR TO THE TEXAS COMPANY, OF HOUSTON, TEXAS, A CORPORATION OF TEXAS.

OIL-CONVERTING- PROCESS FOR THE CONVERSION AND TRANSFORMATION Application filed June 15, 1916. Serial 1%. 103,725.

To all whom it may concern:

Be it known that I, JOSEPH H. ADAMS, a citizen of the United States, residing at Flatbush, in. the county of Kings and State 5 of New York, have invented a new and useful Oil-Converting Process for the Conversion and Transformation of Oils, and of which the following is a specification.

This invention relates broadly' to the art of converting fluids such as oils into products of dissimilar character from the original untreated oils, by heating the oils, vaporizing them under pressure, then cracking and transforming such oily vapors while under vapor pressure into lighter vapors which, as converted and when condensed under pressure, will result in lower boiling products from original high boiling oils.

In its more intense aspect the invention 50 consists in a thermal and vapor pressure method of converting the vapors of semi and ,more or less refined mineral oils as those of the kerosene, non-viscous, neutral, gas, fuel and coal tar oils into more volatile and lower boiling hydrocarbons such as gasolenes, naphthas, benzines, benzol, tuluol and other light oils and oily spirits of both the ali hatic and aromatic series.

he apparatus illustrated and to be described as adapted for use in carrying out my process was invented by me but is not herein claimed since it is made the subject.

matter of another application Serial No. 103,726 filed of even date herewith.

One object of the invention is to formulate a process of a commercial nature for transforming higher boiling oils into lower boiling products by vaporizing the oil, cracking and condensing the vapors while main- 40 taining the whole system under pressure of the generated vapors.

Another object of my invention is to provide a simple and commercial process of cracking or converting high boiling hydrocarbon oil in the vapor phase into lower boiling products, and particularly to insure an efficient and effective conyersion process by preliminarily heating theoil to substantially its boiling or vaporization point under super-atmospheric pressure and then discharging or expanding it into vaporousl form and cracking it in the vapor phase under superatmospheric pressure and crack- 111 temperature, after which the evolved vapors are condensed and collected.

The invention is clearly distinguished from methods of fractional distillation by Wh1ch hydrocarbon oils are. commonly separated into distillates according to the respective boiling points therof, inasmuch as co by the practice of my invention the molecular construction ofthe higher boiling hy drocarbons is transformed so as to produce lower boiling point products.

It has been my purpose to efiect this con od version in the least expensive and most practlcal manner and to that end my process and method embodies broadl some or all of the steps of first heating, t en vaporizing the oil, then cracking and transforming the vapors at elevated temperatures while the OllS and oily vapors are maintained under super-atmospheric vapor pressures, and condensing the vapors under like pressures, the condenser being preferably in free communication with the converter.

In carrying out my invention in its preferred form, the oil is preheated to approxlmately its boiling or vaporization point under sufiicient superatmospheric pressure to maintain it in liquid form. The highly preheated liquid oil to which the latent heat of vaporization has been supplied, in a state of incipient vaporization, is then discharged or released into an enclosed cracking chamber, which is maintained at a cracking temperature and at a superatmospheric pressure somewhat less than that under which the oil is preheated, whereupon the liberated oil expands and breaks into vaporous form in which it is subjected to the full cracking heat of the chamber and effectively cracked or converted in the vapor phase. The cracked vapors pass to a condenser which is maintained at substantially the same pressure as that of the converter, the desired pressure bein maintained by controlling the discharge of liquid and gases from the apparatus. By properly controlling the oil supply and the discharge of the generated products the process may be operated continuously.

Other objects and features of the invention will become apparent to those skilled in the art from the following description of a preferred illustrative embodiment of the invention.

In some cases oils of one series may be transformed into those of an entirely and essentially different series as the aliphatic into the aromatic or the chain into the ring series.

For example, a kerosene or gas oil distillate ielding no gasolene or naphtha by' fractional distillation may, by this vaporizationh eatpressure method, be transformed into gasolene and naphtha, the heavy coal tar oils into benzol, toluol and other lighter oils, while under different conditions, that is higher heats and pressures, petroleum oils may be transformed into aromatic compounds as benzene, be-nzol, toluol and other light oils.

The description of the process is facilitated by means of drawings showing apparatus adapted for carrying out the invention.

Referring to the drawings:

Fig. 1, is an elevation and partly sectional drawing of a simple apparatus adapted for carrying out my process.

Fig. 2, is an elevation and partly sectional drawing of another and more complete apparatus embodying additional details.

Fig. 3, is a partly sectional elevation drawing of a commercial type of apparatus more complete in detail and structure.

Fig. 4, is an elevation drawing of a hattery of vapor converters showing the free communication of the units one with another.

Fig. 5, is a sectional drawing showing the manner of admitting super-heated steam to the oily vapors undergoing transformation.

Fig. 6, illustrates another method of introducing super-heated steam to the oily vapors while being subjected to the powerful influence of cracking heats and high vapor pressures, and:

Fig. 7, is an elevation and partly sect-ional view of the heat exchanger for pre heating ingoing oil the combustion chamber of regenerative furnace and group of vertical vapor converting chambers enclosed within the body of the high temperature furnace.

In Fig. 1., of the drawing a simple form of apparatus is shown embodying the main elements of my invention and in Fig. 2, I have shown an apparatus adapted for carrying out the herein described process and having additional features not shown in Figure 1, while in Figures 3, 4, and 7 I have shown an apparatus of commercial capacity for carrying out my invention on a large scale, Figures 5 and (3 showing details of l igures 3, 4, and 7.

In these figures I have designated the main elements of the apparatus with letters of the alphabet whereas the specific parts are marked with reference numerals, the same reference characters being used to indicate corresponding parts in the three fig ures.

Referring particularly to the simple form of apparatus shown in Fig. 1, the reference character A, represents an oil supply tank from which the oil is supplied to the apparatus for the conversion process.

The oil passes from this tank A, through pipe 4, precision feed valves 6' and pipe 6, to pro-heater B, in the coils or pipes 7 of which the oil is heated, then through pipe 8, to the tubes 9 and chamber 10 of converter C, where the hot oil breaks into spray or mist like vapor so that in such gaseous form it may come in contact with cracking heats within thetube coil 9 and chamber 10.

The pre-heater B, is of any preferred construction as a feed water heater, a small boiler or other form of heat-er, whereby the, oil may be heated by suitable means in order to raise it in temperature substantially to, or approaching, the boiling or vaporizing point under the particular pressure employed, so that when admitted or sprayed into the cracking chamber or tubes it will break into vaporous form.

The converter C, embodies an outer casing 35, of heat enduring and insulating material for confining the heat and any suit-- able means may be provided for heating this chamber, such as oil or gas burners or other economical means of fuel consumption. I prefer making the converter itself in tubular form so that there will be a large heating surface presented as compared to the volume of vapor undergoing conversion passing through the converter; and in the form shown in Fig. 1, the converter C comprises a pipe coil 9 and an enlarged chamber 10. The oil preheated under pressure to substantially its vaporization point, at that pressure in the preheater B, is delivered through valve 26 in a thin stream into the bottom of the coil 9 through which it rises and is then admitted-into the enlarged chamber 10. Both the coil 9 and the chamber 10 are heated to intense cracking temperatures which are in excess of the temperature of the preheater, Therefore, as the oil, in a state of incipient vaporization, rises through the pipe 9 and into the. enlarged chamber 10, the relation of heat to pressure is such that the oil in transit will break into and maintain a vaporous. form in which it is cracked.

The vapors, after being subjected to the high temperature in the coils 9 and the enlarged chamber 10, pass out through pipe 11., to separating chamber 12, where the lighter converted vapors rise and flow through pipe 13, to condenser D, where, in the coils 14, the vapors are passed down and asaevv condensed to liquid: and, together with the fixed gases generated during the process, are drawn off through pipe 15 and valve 16, into running trap tank E, which is provided with a draw oil pipe 17 controlled by valve 18. t

It will be understood that the supply tank A, can be re-filled from time to time through the inlet pipe 1, and that th supply of oil from that tank to the converter 0, may be augmented by air pressure which is applied over the surface of oil in the tank in order to force it into the pre-heater B, and so on into the converter C, the valve 2, being closed as well as the valve in vent pipe 3, and the air pressure being registered on pressure gauge 33.

The compressed air may be supplied from any suitable source (not shown) and may conveniently be introduced through the pipe 3 if desired. Sufficient pressure is thus maintained upon the supply of oil to force it through the preheater against the back pressure of the converter and to hold the heated oil in liquid form while being raised to substantially its corresponding boiling point and until it is introduced by releasing or spraying it into the converter in which it. immediately vaporizes and is cracked.

The pre-heater B, is intended only to heat the oil sufficiently to cause its easy vaporization when admitted to the converting chamber or coils 9, through pipe 6, and is not intended to perform any cracking operation;

the heated oils at the time of admission to the said chamber then being at a temperature suiiicient to immediately vaporize and expand them for the vapor conversion process.

The temperature of the converter C, is raised to such a point as will crack or convert the oily vapors into lower boilingproducts or convert them into products having essentially different natures.

By reason of the preheating of the oil to substantially its vaporization point, the heat of the converter is fully expended in effectively cracking the oil in the vapor phase.

It will be seen that the condenser D, is in open communication with the converter 0, through pipe 11, and separator 12, and therefore any pressure in the converter will extend to and through the condenser.

The continual feeding of new quantities of hot oil to the apparatus will build up or raise the vapor pressures in the converter; and consequently throughout the condenser, so that the vapors undergoing the cracking operation will at all times be under superatmospheric pressures while being subjected to cracking heats. This pressure is of course the result of the expansion due to the vaporization and heat and is somewhat less than that utilized to force the oil ghrough the preheater and hold it in liquid orm.

This pressure maintained in the converter and through the condenser may be regulated by controlling the discharge of the fixed gases which are always generated to a more or less extent in the converter.

The condensation of 'vapors also tends to reduce'the pressure and thus control of the escape of fixed gases is-suflicient to enable the operator to maintain the pressure de sired.

The fixed gases pass outwith the con densed vapors through the pipe 15, into the trap tank E, and their escape through the pipe 19, is controlled by valve 20.

When the process is in operation pressure in the converting system will be registered on gauges 30 and 32, which, under normal operative conditions, should both indicate the same uniform pressure, while for safety purposes in this hi h pressure system, comprising pre-heater converter (1, condenser D and the running trap tank E, the release blow off valve 21, is provided and located about over the condenser D.

The gauges 30 and 32, register vapor pi-essures while in this form of apparatus gauge 31, on the pre-heater B, registers the oil pressure which in all cases should be below the pressure maintained over the oil in supply tank A, as registered on gauge 33.

Vapors which pass out from the expansion chamber 10, through pipe 11, and into the separator column 12, may there be separated into the lighter ones, which pass to the condenser D, and heavier partially or wholly unconverted vapors which will drop to the bottom of the column together with particles of coke or carbon.

The bottom of this chamber 12, isconnected to overflow hot oil tank G. by means of pipe 22, the flow of oil through which is regulated and governed by valve 23, and this column 12, is alsoprovided with a detachable plate 24, so that solid or semi-solid matter and deposit may be removed from time to time. The material collecting in the tank G may be returned to the supply tank for further treatment, the pump H serving to draw off the oil through the line 25 and return it to the tank A through the line 34:.

The drawing Fig. 2, presents a partly sectional elevation of an apparatus adapted to carry out my process embodying a suit-able oil suply tank A, and air pressure pump H, to maintain pressure over the surface of oil in the tank in order to force itinto converter C, through pre-heater B, against a high back or vapor pressure while maintaining it in liquid form; a converter C, in tubular form enclosed within a hi h temperature furnace 35, a condenser D, and liquid running trap E, in free communication with the converter, an enclosed running tank F, for the distillates of converted oils connected with the trap E and tank G, for partly or wholly unconverted oils which may be removed from time to time from the lower or heavy bottoms chamber 29, and returned through pipe and pump H, to supply tank A, for retreatment. These parts correspond in operation to similar parts shown in Fig. 1.

The drawing Fig. 2, shows one of the many forms of tubular converters which may be employed in my process.

At the upper end of the tube 9, an expansion chamber 10, permits the lighter converted vapors to become more or less sepa rated from the heavier ones and pass out through the vapor pipe 11, to condenser D,

, while the heavier partially or wholly unconverted vapors drop back and down through the tube 9, for further treatment, while the very heavy ends as well as any carbon cracked out in mineral form may precipitate or fall into the heavy bottoms chamber 29,-located below the tube.

This chamber 29, is connected to overflow oil tank G, by means of pipe 22, regulated by valve 23, and is provided with a detachable plate 24, so that solid matter may be removed at times as required.

The heated oil is delivered by spraying it in'at the upper end of cracking tube 9,

through a perforated collar or circular nozzle 27, which, with its own heat and the intense temperature of the converter, drives the oil into a vapor or mist like condition ready for contact with the cracking heats while held under super-atmospheric pressures during the process.

As the oily vapors pass down through the tube 9, a part or all of them are converted into lower boiling products and While some of them flow out through pipe 11, leading from the upper expansion chamber 10, others flow through pipe 12, leading from the lower or heavy bottoms chamber 29 and through the condenser D. This pipe connection furnishes free and open communication between the converter C and the condenser D and permits an. equalization of pressure. I

As an added 28, provided with a helical strip of metal feature of importance in this vertical K type of tubular converter a rotor the cracked vapors or precipitated therefrom will drop into the heavy bottoms chamber 29, through tube 9, or pipe 12, so that vapors led into condenser D, may be in part or wholly freed from mineral carbon; and any carbon adhering to the inside of the vertical tube may, by means of the revolving rotor 28, be nipped off and caused to drop into the chamber 29, below the tube.

Referring now to the drawing Fig. 3, the source of supply or oil tank A, may be located at any required distance from the preheater B, and by means of pump 5, the oil is delivered continuously into the tubes 9, of converter C, through the heating coils 7 and pipe 8, to replace that which is continually withdrawn from the converter in the form of vapors.

Pump 5, is provided to draw oil through pipe 4., and force it through precision valves 6, pipe 6, pre-heater coils 7 and pipe 8, into the tops of converting tubes 9, of converter C.

It is alwaysbest to pre-heat original oil before admitting it to the vaporizing system so that the heat from the furnace may be conserved for the purpose of cracking the vapors of oils and not for pre-heating it to a cracking temperature: and to this end the'waste heat from the furnace as it escapes through flue 71, into the throat g, of stack 50, can be economically applied in this form of exchanger to the purpose of heating original inflowing oil through pipe coils 7.

The oil so heated is forced into the tubes of converter C, through pipe 8, which delivers it to the several spray nozzles 27, at the heads of the tube connections against a back or generated vapor pressure maintained in the tubes 9, and throughout the several following parts of the system comprising the carbon and vapor chamber 29, the tubes 14 of condenser D, running trap tank E, and the intervening vapor and liquid pipes 12 and 13, 15 and 17 valve 16 and both sight glasses and pressure gauges located on the apparatus.

This drawing Fig. 3, shows one of the many forms of tubular converters which may be employed in my process, and in this type of apparatus a multiple of heat enduring tubes 9, constructed of materials capable of withstanding intense temperatures and high pressures are located vertically in the high temperature furnace and enclosed within fire brick Walls 35, designed to withstand protracted high temperatures and.

cracking heats. These chambers or tubes 9, are connected into a header or heavy bottoms chamber 29, at their lower ends and are assembled in groups attached to each header 29, so that the entire group composed of two or more headers may receive the greatest efficiency from the furnace heat well as the which may be generated in a primary cham her and passed 1nto this furnace of converter rangement facilitates the efiiciency of the process.

At the lower outgoing ends of the series of tubular chambers 9, vapors are led into a carbon and oil vapor trap 29, where any free carbon accummulated during the process is swept by the current of oily vapors in the tubes. This trap 29, is provided with detachable plates 24, at its ends for cleaning out purposes and leading-from one or both ends of the chamber a vapor-pipe 12, conducts light converted vapors to coils 14, of condenser D.

Any free carbon which may be held in suspension in vapors issuing from the converting tubes 9, may have a chance to precipitate to the bottom of this header or trap 29, and

from vapor line 12, while vapors are rising therein so that vapors led into the condenser D, may be in part or wholly freed from mineral carbon.

Any oils or condensed vapors caught in the bottom of trap 29, may be intermittently or continuously withdrawn through pipe 22 and valve 23 into hot oil collecting tank G, from which they may be withdrawn through pipe 25, b pump H, and returned to oil supply tan through pipe 34. y

The vapor line 12, rising from one end of the chamber 29, conducts vapor into the coils or pipes 14, of condenser D, which latter may assume any of the forms employed in the oil refining industry.

- The coils or pipes 14 of condensing apparatus D, are ordinarily iminersed 1n cold water and the rapidity of condensation as uality of product can be partially controlled by the temperature of the water surrounding these condensing coils or 1 es. p ondensate accumulated in the condenser runs without interruption into an enclosed collecting or running trap tank E, freely connected therewith by pipe 15 and valve 16, from which it is withdrawn into running tank F, through pipe 17 and valve 18, after passing sight box 40.

Any accumulation of distillate in the tank F, may be drawn off through pipe41 and valve 42, to make room for newly and continuously admitted distillates from trap tank E;

The vapor pressure is indicated and regulated as in the form shown in Fig. 1.

In feeding oil to the system through pump 5, the pump cannot be so accurately regulated as to constantly deliver the required amount of oil into the converter chambers, therefore a return pipe 43 and enclosed pop or release valve 44, will permit any excess oil not delivered into the system to be returned to the supply tank A.

This pop valve 44, can be set at any tension ten or fifteen pounds or more greater than the pre-determined number of pounds pressure maintained in the system and with the pump 5, operating under normal conditions all oil not delivered through the precision valves 6, will be returned under pressure to the tank A, through the release valve 44, and such pressures may be constantly known and under observation by means of gauge 33, arranged in the excess oil line 43, so as-to be constantly informed as to the conditions under which the pump 5, is working.

Thermometers and pyrometers a, b, c, d, e and f, are placed at several important locations on the apparatus so that a comprehensive idea may-be had as to temperatures of heats, vapors, steam etc.

A feature of primary importance in this invention is simplicit in the operation of the process in a suitab e apparatus as well as the rapid, continuous and safe method of oil and oily vapor transformation to produce large yields of low boiling hydro-carbons and other oily products.

The multiplicity of tubular converters present large surfaces to the furnace heats in proportion to the amount of oil in vapor form contained in the tubes, and thus the yield of light distillates will be rapid and the quality high in desired products.

A considerable number of tubes having a comparatively small diameter of from two to eight inches may be so arranged as to present from four to six times greater surfaces to the intense furnace heat than the parts of tubes extending through and beyond the furnace walls for terminal and return fittings, if such an arrangement is employed.

When the supply pump 5, is 1n operat1on oil will be constantly flowing under pressure through the coils 7, of pre-heaterB, into the cracking chambers, being admitted through spray nozzles 27. The spray or vapors takes the place of that already converted and condensed.

This newly admitted o1ly spray or vapor will in turn be superheated, cracked and sub-divided into finer vapors and changed in the apparatus into lighter or more volatile products by splitting the molecules of or rearranging them and breakmg out a small portion of carbon.

In this manner the complex mixture of oils known commercially as kerosene, gas,

character of the vapors may possibly be changed from one or more of the products of the hydro-carbon series into others of an essentially different character and series.

The carbon which is removed in this manner will be in part deposited in the tubular converters and in part precipitated in the carbon and vapor trap 29, as the certain small ortion broken out in the process may be held in suspension in the vapors during a part of their course through the converting tubes 9, and adjacent pipes and condens ing tubes 14, of apparatus D.

The continual circulation of o1ly vapors through the tubes permits the intense heat to act rapidly and convert high percentages of the subjected vapors into desired products and the small quantity of vapors contained within such tubes, traps, cooling coils and vapor lines assures a certain degree of safety in the operation of this apparatus for if a break should occur in any part of the converting system under pressure, the fire which might result would be confined principally to a very few barrels or gallons of oil in vapor form undergoing treatment rather than a still full of liquid material.

The furnace of converter C, may be operated in any convenient manner with coal, fuel oil, gas, electricity or other economical and easily obtainable heat producing medium, but for uniformity of result, economy .and generally satisfactory operation, a fuel oil burnir-g equipment is at thg present time and for general localities, the most practical method of generating intense temperatures such as are required in the furnace of this converter.

' Almost any of the efiicient oilburning systems are adapted to this workbut as that part of the apparatus is not a feature of this process any specific description is avoided beyond the indication of a burner projecting into the opening is, of the combustion chamber 45, of Fig. 7, the fiues j and It, and in the location of the stack 50, rising from the side or rear of the converter 0, for draught or vent purposes.

As a feature of safety in this high temperature and pressure rocess the release blow off valve 21, is pre erably located at a distance away from the converter, usually Any tendency toward a drop in pressure in one converter will be compensated for by the pressure from the others and thus easier and more perfect regulation may be secured.

This arrangement is shown in Fig. 4, where a battery of converters C-C-C, are spaced apart the required distance for mechanical operation and the proper arrangement of connecting pipes and pipe connections, the hot oil being forced through pipe 8, and delivered to the tubular-converting chambers 9, in each of the converters.

The converted and transformed vapors pass out through traps 29, into the vapor line 12, leading to the condenser where they are reduced to distillates in the tubes 14.

As each one of the tubular converting units comprising the chambers 9, are freely connected with the vapor line 13, by means of the pipes 12, leading out from the top of traps 29, and this vapor line leads freely to and is in open communication with. the

condenser in which vapors are condensed under vapor pressures maintained throughout the converting system, it will be seen that two or more converters comprising a battery will be equalized in operative vapor pressure through the vapor line 13, or other vapor lines which may be employed to con-. meet and compensate the several converters for the purpose of equalizing and maintain- -ing uniform pressures in the vapors undergoing transformation in such a battery of converters.

This unit battery feature and the freely connected converters one with another, in its broadest aspect was first adopted by me and employed as described in my co-pending application Serial No. 530,852, filed Dec. 1, 1909, which matured on October 28, 1919, into Patent 1,320,354, and is claimed in Patent 1,433,519, which is a division of said patent and was granted on October 24, 1922.

As an added feature of importance in this method of oily vapor transformation I may also use super-heated steam injected while at elevated temperatures into the body of oily vapors through one or more of the tubular converters 9, as indicated by the pipev 4:6, and jets 47, shown in Fig. 3, and on a larger scale in Figs. 5 and 6, the steam being generated outside the apparatus but mitted from outside and controlled in its entry into the oily vapors by valve 49.

The pipes 47, employed for such admission of steam may be more clearly seen in the drawing Fig. 5, where one is shown projected into the top of an oil inlet and return bend connecting two tubes, the steam flowing through pipe 46, and admitted to the interior of the converters by pipe 47 and a small perforated jet 38, at the bottom of the pipe through which the super-heated and gaseous steam .is forced under higher pressure than that maintained in the converting system.

As a matter of convenience and mechanical practicability, I may also introduce the steam into tubes 9, by projecting the steam pipe or pipes 47, into the end of one or more tubes, as shown in Fig. 6, carrying it down a part of or all of thelength of each tube and providing the pipe with suitable openings or jets 39, for the proper admission of steam, which same is controlled by valve 49. I ordinarily super-heat the steam above 800 to 1000 F. and when admitted and mixed with oil and oily vapors it possesses advantages both in hydrogenating oils and reducing mineral carbon deposit while at thesame time the resultant distillates are superior in odor and color, and I therefore intend that this feature may be employed in this process as a matter of practical and mechanical convenience at such times as the operator may find it advisable to introduce the same for the purposes described.

I may also employ rotors 28, in these vertical tubes as shown at the left side of Fig. 5, and install them as shown in Fig. 2, for the principal object of removing carbon from the interior of the tubes 9.

Having filled the reservoir tank or source of supply A, with original oil to be converted the fires are started in the furnace of converter 0. Oil is admitted into the converting chambers 9, in small sprayed or vaporized quantities continuously, and as it falls through the chambers, becomes super-heated and is withdrawn through pipe 12, into the condenser D, and any heavier un-converted liquid portions which fall into the chamber 29, are drawn off from time to time or continuously and returned by pump H, .to the supply tank A, until the coil 7, in the preheater B, has been raised in temperature sufficient to bring the oil to its boiling point under the pressure maintained in the preheater, and the tubes are heated to vapor cracking temperatures which may be determined by the pyrometer installed in the system, and the vapor pressure in the converter and condenser begins to rise.

The temperatures should finally be sufficiently elevated to prevent condensation of vapors while contained in the tubes and as soon as the tubes 9, are full of vapors and the temperature increased until it reaches the required cracking heat it is then maintained at that temperature which will render the bestconversion results continuously while the vapors are held under vapor pressures.

In this operation some of the vapors will necessarily be changed to fixed gases and some of the vapors will not be converted but a large proportion will be converted into lower boiling products essentially different in nature from the original material.

lVhen the products pass from the converting tubes 9, into the trap 29, some of the un converted oils of high boiling point will condense and may be drawn off through pipe 22 and Valve 28, while the converted vapors and fixed gases will rise through pipe 12, and pass into the coils 14, of the condenser D. The converted vapors are here condensed and pass with the fixed gases into the trap tank E, from which they are drawn oil in liquid form into tank F, through pipe 17 and valve 18.

The fixed gases are carried off by pipe 19, and the valve 20, in that pipe may be so adjusted as to allow the escape of so much gas as will maintain the desired pressure in the converter and condenser.

Preferably the process is operated as a continuous one, oil being continuously supplied from tank A, through preheater B. to the converted C. I or spreading the hot oil into the converter where it immediately vaporizes and the generated self-imposed pressure of the vapors due to the cracking operation tend, of course, to ra1se the pressure in the converter but this is compensated for by the condensation of the vapors in the condenser and the regulated escape of fixed gases and thus, even in the continuous operation, the pressure may be maintained at the number of pounds desired throughout the continuous use of the process.

It will be understood by those skilled in the art that the temperature necessary in the pre-heater B, converter C, and the pressure of the vapors in the converter through the condenser will vary with the characteristics of the particular oil being treated and therefore it is not possible to state any definite figures which would be applicable to all oils. The operator may determine when he gets the proper temperature in the con- The operation of forcing verter by the character of the product comthat a kerosene distillate with an initial boil- 7 ing point of 300 F. can be converted into distillate having an initial boiling point below 100 F. and a heavy paralline gas oil having an initial boiling point of 400 to 500 F.'can be converted into a distillate having a boiling point of 100 F. or less.

If, in the use of my process, it is desiredto secure the greatest yield of gasolene the operation should be so regulated as to obtain a converted product having an initial boiling point of 100 F. or less.

Subject to variations, in accordance with the particular oils and operating conditions, I now believe that the present process of oil conversion is preferably conducted at temperatures from 1000 to 1200 F. and at pressures of from 70 to 90 pounds in the cracking converter. The temperatures might in some cases run as low as, or even lower than 900 F. or as high as 1500 F., while the operating pressures might range between 50 and 100 pounds or even considerably higher. The process, however, is primarily a vapor phase process and, therefore, the operating temperatures preferably will be some what higher than those commonly employed in processes of oil conversion in the liquid phase.

"While it is possible to bring about these changes and convert higher into lower boiling compounds it is impossible to broadly state specific pressures and temperatures applieable to oils in general. as the natures of crude hydro-carbons as well as the distillates of crude oils vary so greatly in their composition and qualities that it is impossible to apply a fixed rule to oils in general and particularly to those which as a matter of commercial advantage would be available for conversion by the application to them of this process. I The present invention relating to the process is. of course, not limited to the use of aspecific apparatus and it may be performed in *arious ways. I believe the fundamental steps of the process above set forth to be broadly new and by the language employed in the following claims it is my intention to cover that process in its broadest aspect.

Having described my invention what I claim as new and desire to secure by Letters Patent is:

1. A process of converting high boiling hydrocarbon oil into lower boiling products in the vapor phase comprising heating the oil in a preheater under super-atmospheric pressure to substantially its corresponding boiling point, delivering the heated oil into a chamber where it breaks into vaporous form, maintaining substantially the same superatmospheric pressure on the oil vapors in the chamber and subjecting the oil vapors therein to a cracking temperature whereby the oil is converted in the vapor phase.

2. A process of converting high boiling hydrocarbon oil into lower boiling products in the vapor phase comprising heating the oil in a preheater to substantially its boiling point under sufficient superatmospheric pressure to maintain it in liquid form, releasing the heated liquid oil into an enclosed chamber where it breaks into vaporous form, maintaining on the vapors in the chamber substantially the same superatmospheric pressure and subjecting the vapors in the chamber to cracking temperature to ellect a conversion thereof in the vapor phase.

3. A process of converting high-boiling hydrocarbon oil into lower boiling products in the vapor phase comprising continuously supplying oil under superatmospheric pressure in a confined stream, heating the oil in a preheater as it passes to substantially its boiling point corresl' onding to the pressure employed while still maintaining it in liquid form, discharging the heated liquid oil into an enclosed chamber where it breaks into vaporous form, and maintaining the oil vapors under subst:-1ntially the same superatmospheric pressure and at'a cracking temperature whereby they are converted in the vapor phase.

at. A process of converting high boiling hydrocarbon oil into lower boiling products in the vapor phase comprising preliminarily heating the oil in a preheater to a point of incipient vaporization, dischargingfit in, vaporous form into a chamber, heating the vapors therein to a cracking temperature, conveying the evolved vapors through a condenser in open communication with the chamber and so'regulating the discharge of the resultant product to maintain a substantially uniform superatmospheric pressure in the condenser and the chamber.

5. A process of converting high boiling hydrocarbon oil into lower boiling products in the Vapor phase comprising heating the oil in a preheater under superatmospherie pressure to substantially its corresponding boiling point while maintaining the oil in liquid form, admitting the preheated liquid into a chamber under superatmospheric pressure somewhat less than the pressure under which the oil is preliminarily heat-ed, where it breaks into vaporous form, and subjecting the vapors in the chamber to' a cracking temperature to convert them in the vapor phase.

6. A process of converting high boiling hydrocarbon oil into lower boiling products in the vapor phase comprising heating the oil in a preheater under superatmospheric pressure to substantially its boiling point at that pressure, delivering the heated oil in vaporous form into a confined chamber, subjeeting the oil vapors therein to superatmospheric pressure and to a cracking temperature whereby the oil is converted in the vapor phase and condensing the converted vapors under superatmospheric pressure.-

A process of converting high boiling hydrocarbon oil into lower boiling products in the vapor phase comprising heating the oil in a preheater under s'uperatmospheric pressure to substantially its boiling point at that pressure While maintaining it in liquid form, delivering the heated oilin vaporous orm into an enclosed chamber against a back pressure, subjecting the oil vapors therein to a slightly reduced superatmospheric pressure, heating the oil vapors while under said pressure to a temperature sufficient to effect their conversion and condensing the resultant product under superatmospheric pressure.

8. A process of converting high boiling hydrocarbon oil into ldweriboiling products in the vapor phase comprising continuously heating the oil in a preheater under superatmospheric pressure to substantially its boiling point while maintaining it in liquid form, continuously delivering the heated oilinto an enclosed chamber and against a back pressure when the oil breaks into vaporous form, subjecting the oil vapors therein to a slightly reduced superatmospheric pressure, heating the compressed vapors to a cracking temperature and con'' densing the converted vapors under super atmospheric pressure and in open communication with the compressed vapors undergoing conversion whereby the 011 is converted and condensed at a substantially uniform superatmospheric pressure.

f 9. A process of converting high boiling hydrocarbon oil into lower boiling products in the vapor phase comprising heating the oil in a preheater under superatmospheric pressure to substantially its boiling point, delivering the heated oil in vaporous form within an enclosed chamber, maintaining the oil vapors therein under substantially the same superatmospheric vapor pressure, subjecting the vapors under pressure to a cracking temperature to convertithe oil in the vapor phase, condensing the converted products under said superatmospheric vapor pressure and collecting the resultant low boiling condensate.

10, A process of converting high boiling hydrocarbon oil into lower boiling prodnets in the vapor phase comprising preliminarily heating the oil in a preheater under superatmospheric pressure to a point of incipient vaporization, delivering the oil in vaporous form into an enclosed chamber and against a back pressure, maintaining the oil'vapors in the chamber under a slightly reduced self-imposed superatmospheric vapor pressure, subjecting the oil vapors while under pressure to a cracking temperature, causing the oil in vaporous form to flow continuously through the chamber while subto substantially its bo1ling point and delivering it 1n vaporous form into an enclosed chamber and against back vapor pressure, subjecting the oil vapors in the chamber to suflicient superatmospheric vapor pressure and temperature to efi'ect their conversion, condensing the converted vapors under said superatmospheric vapor pressure and returning the artially or wholly unconverted oil to the chamber for retreatment.

12. A process of converting high boiling hydrocarbon oil into lower boiling products in the vapor phase comprising preheating the oil in a preheater under superatmospheric pressure to substantially its corresponding boiling point while maintaining it in liquid form delivering it to an enclosed chamber subjected to substantially the same superatmospheric pressure-and to a cracking temperature whereby the oil breaks into vaporous form and is converted in the vapor phase, withdrawing and condensing the converted products as they are evolved and removing from the cracking zone'the carbon pheric pressure to substantially its corre sponding boiling point while maintaining it in'liquid form, spraying the heated liquid 'oil in vaporous form into the top of an enclosed chamber and subjecting the oil vapors l in the chamber to a cracking temperature and to substantially thesame superatmospheric pressure whereby the vapors are cracked and converted.

14. A process of converting high boiling hydrocarbon oil into lower boiling products in the vapor phase comprising preheating the oil under superatmospheri pressure to substantially its corresponding boiling point while maintaining it in liquid form, delivering the heated oil in vaporous form into the top of an enclosed chamber, delivering steam into the chamber concurrently with the heated oil and heating the mixed vapors and steam in the chamber to a cracking temperature while maintaining them under superatmospheric pressure whereby the oil is cracked and converted in the vapor phase.

15 A process of converting hydrocarbon oil into lower boiling products in the vapor phase, comprising preheating a continuously moving stream of oil under superatmospheric pressure to a point of incipient vaporization, continuously spraying said heated oil, to-

I gether with superheated steam, into an enclosed chamber in mist-like vaporous form, heating the vapors in said chamber to a cracking temperature while maintaining a superatmospheric pressure insufficient to hold them in liquid form at the temperature employed, and drawing 0E and condensing the cracked vapors.

v 16. A continuous process of converting high boiling hydrocarbon oil into lower boiling products in the vapor phase, that comprises heating a continuously moving stream of oil under superatmospheric pressure to substantially its corresponding boiling point while maintaining it in liquid form, continuously spraying said heated oil in vaporous form, togetherwith superheated steam, downwardly into an enclosed chamber, heating the vapors in the chamber to a cracking temperature while maintaining a superatmospheric pressure insufiicient to condense the lighter vapors at the temperature employed, removing the residue material from the lower part of the chamber, and withdrawing the lighter vapors from the upper -part of the chamber and condensing them, while maintaining substantially the same' pressure as in the chamber during the condensation.

17. A continuous process of converting high boiling hydrocarbon oil into lower boiling products, that comprises continuously heating a moving stream of oilunder superatmospheric pressure to a point of incipient vaporization, spraying the heated oil into the top of said chamber where it breaks into vaporous form, spraying superheated steam into said chamber Where it mixes with the vaporous oil, heating said chamber and its contained vapors below its upper end and above its lower end to a cracking temperature while maintaining a superatmospheric pressure on the vapors insufiicient to condense the lighter vapors at the temperature employed, continuously rem oving the generated carbon and heavy residue downwardly out of the heating zone where it is collected, withdrawing the heavy residue, including the carbon, so collected below the heating zone, and withdrawing the cracked vapors evolved in the heating zone and condensing them under superatmospheric pressure.

18. A process for converting high boiling hydrocarbon oil into lower boiling products that comprises externally heating a plurality of vertical converter tubes to a cracking temperature, forcibly delivering oil from a supply tank to the upper ends of said converter tubes and passing the oil therethrough to be cracked in transit, collecting carbon and heavy residue at the lower ends of said converter tubes, separately removing the evolved vapors and unconverted liquid oil from the lower ends of said converter tubes, returning the unconverted liquid oil to the supply tank for retreatment and maintaining superatmospheric pressure upon the oil under treatment. I

19. A process for converting high boiling hydrocarbon oil into lower boiling products that comprises externally heating a plurality of vertical converter tubes intermediate their ends to a cracking temperature, forcibly delivering oil to the upper ends of said converter tubes and passing it therethrough to be cracked in transit, collecting carbon and heavy residue at the lower ends of said converter tubes, removing the evolved Vapors from the lower ends of said converter tubes and effecting their condensation, and maintaining superatmospheric vapor pressure upon the oil in process of conversion and condensation.

'20. A process of converting high boiling hydrocarbon oil into lower boiling products that comprises externally heating a plurality of vertical converter tubes intermediate their ends to cracking temperatures, forcibly delivering oil from a supply tank to the upper ends of the converter tubes and passing it in flowing streams therethrough to be cracked in transit, collecting carbon and heavy residue emerging from the lower ends of. said converter tubes, removing evolved vapors from the lower ends of said converter tube-s and efiecting their condensation, sep arately withdrawing unconvertedliquid oil from the lower ends of said converter tubes and returning it to the supply tank for retreatment, and maintaining superatmospheric vapor pressure on the oil under treatment throughout the system.

21. A process for converting high boiling hydrocarbon oil into lower boiling products that comprises externally heating a vertically disposed converter intermediate its ends to a cracking temperature, forcibly delivering oil to the upper end of said converter in sprayed or vapor form and passing it therethrough to be cracked in transit, preheating the delivered oil before its introduction into a converter, delivering superheated steam into the upper end of the converter in commingled relation with the sprayed oil, collecting carbon and heavy residue emerging from the lower end of said converter, removing the evolved vapors from the converter and effecting their condensation and maintaining superatmospheric pressure upon the oil during its preheating, conversion and condensation.

22. A- process of converting high boiling hydrocarbon oil into lower boiling products that comprises continuously passing oil under pressure in flowing streams through a battery of converters independently, sepanacaerv rately heating the respective converters of the battery to cracking temperatures, subjecting the oil in the several converters to superatmospheric pressure, equalizing the pressures in the several converters by maintaining free and open communication between the vapor spaces thereof, separately removing the evolved vapors from the re spective converters and delivering them to a common yapor line and condensing the lianpors received from the common vapor on oil into lower boiling products that comprises continuously passing oil under pressure in flowing streams through a battery of converters independently, separately heating the respective converters of the battery to cracking temperatures, subjecting the oil in the several converters to superatmospheric pressure, equalizing the pressures in the several converters by maintaining free and, open communication be tween the vapor spaces thereof and removing and condensing the vapors evolved in said converters.

24. A process of converting high boiling hydrocarbon oil into lower boiling products that comprises separately charging oil in flowing streams through a battery of converters independently heated to cracking temperatures under superatmospheric pressure, e ualizing the superatmospheric pressures i the several converters by maintainmg their vapor spaces in free and open communication, separately removing the vapors evolved in said converters and separately withdrawing unconverted liquid oil fromthe converters.

25. A process of converting high boiling hydrocarbon oil into lower boiling products that comprises forcing oil from a supply tank through a battery oi converters independently and in flowing streams, independently heating the converters of the battery to cracking temperatures under superatmospheric pressures, to efiect conversion of the oil in transit therethiough separately removing the vapors evolved in the several converters and returning unconverted liquid oil from the several converters to the supply tank for retreatment. a

26. Aprocess of converting high boiling hydrocarbon oil into lower boiling products that comprises independently charging oil in flowing streams through a battery of converters separately heated to cracking temperatures under superatmospheric pressures, equalizing the pressure in the several converters by maintaining free and open communication between the vapor spaces thereof, independently removing the evolved vapors from the several converters and delivering them to a common vapor line sepa- 23. A process o fconverting high boiling hydrocar rately removing unconverted liquid oil from said converters and delivering it to a common oil line.

27. A process of converting high boiling hydrocarbon oil into lower boiling products that comprises delivering oil from a supply tank to a battery of converters independently and passing the oil therethrough in flowing streams, independently heating the several converters to cracking temperatures under superatmospheric pressures, equalizing the pressures within the several converters by freely connecting the vapor spaces thereof, separately removing the evolved vapors from the several converters and subjecting them in common to condensation, independently withdrawing unconverted liquid oil from the several converters and returning it to the supply tank for retreatment.

28. A process of converting high boiling hydrocarbon oil into lower boiling products that comprises forcibly delivering oil from a supply tank, to one end of a plurality of vertical converter tubes and passing it therethrough in flowing streams to be cracked in transit, heating the converter tubes intermediate their ends to a cracking temperature under superatmospheric pressure, withdrawing unconverted liquid oil from the opposite ends of said vertical converter tubes and returning it to mix with the oil in said supply tank for retreatment and removing the vapors evolved in the converter tubes.

29. A process of converting high boiling hydrocarbon oil into lower boiling products that comprises forcibly delivering oil from a supply tank to one end of a plurality of vertical converter tubes and passing it therethrough in flowing" streams to be cracked in transit, heating the converter tubes intermediate their ends to a cracking temperature under superatmospheric pressure, withdrawing unconverted liquid oil from the opposite ends of said vertical converter tubes and returning it to mix with the oil in said supply tank tor-retreatment,

till

llllil removing the vapors evolved in the converter tubes, and collecting below the heating zone carbon and heavy residue formed in said converter tubes and emerging from oil in said supply tank for retreat-merit, removing the vapors evolved in the converter tubes, collecting below the heating zone carbon and heavy residue formed in'said converter tubes and emerging from the lower ends thereof, and supplying fresh oil to the system during the operation thereof to compensate for the removal of evolved vapors.

31, A process of converting high boiling hydrocarbon oil into lower boiling products that comprises delivering oil from a supply tank to the upper ends of a plurality of vertical converter tubes, and forcibly passing it downwardly therethrough in flowing streams to assist the action of gravity in carrying carbon downwardly through said converter tubes, heating the converter tubes intermediate their ends to a cracking temperature under superatmospheric pressure to convert the oil in transit, collecting below the heating zone carbon descending from the vertical converter tubes, returning unconverted oil from the lower ends of the converter tubes to the supply tank for retreatment and removing from the system forcibly passing it under superatmospheric pressure therethrough in flowing streams to be cracked in transit, heating the vertical converter tubes intermediate their ends to a cracking temperature whereby the oil is converted 1n its passage therethrough, collecting carbon and heavy residue below the heatin zone, withdrawing unconverted liquid oi from the exit ends of the vertical converter tubes and removing from the systdm the vapors evolved during the cracking operation. I

In testimony whereof I afiix my signature in the presence of two witnesses.

JOSEPH H. ADAMS. Witnesses:

A. CAPSTICK,

J. S. DE SELDING 

